US4378336A - Monolith reactor - Google Patents
Monolith reactor Download PDFInfo
- Publication number
- US4378336A US4378336A US06/341,946 US34194682A US4378336A US 4378336 A US4378336 A US 4378336A US 34194682 A US34194682 A US 34194682A US 4378336 A US4378336 A US 4378336A
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- Prior art keywords
- passageways
- reactor
- channels
- passageway
- monolithic substrate
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/248—Reactors comprising multiple separated flow channels
- B01J19/2485—Monolithic reactors
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00026—Controlling or regulating the heat exchange system
- B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
- B01J2208/00088—Flow rate measurement
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/0015—Plates; Cylinders
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
- B01J2208/00221—Plates; Jackets; Cylinders comprising baffles for guiding the flow of the heat exchange medium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
Definitions
- This invention relates to apparatus comprising monolithic substrate reactors for use in automobiles in the on-board production of hydrogen fuel from methanol.
- improved reaction conditions of increased catalyst contact area are obtained.
- the passageways may have catalysts coated on the inner surface thereof.
- catalysts as copper/zinc would be used to coat the inner surface of the passageways, or be used as the catalyst in the catalytic pellets contained and supported within the passageways.
- the invention relates to a method for fueling an internal combustion engine with methanol decomposition products. This method is carried out using standard vaporizing and reacting steps whereby liquid methanol is first vaporized and then reacted over a suitable reforming catalyst such as copper/zinc to produce carbon monoxide and hydrogen. These gaseous products are then charged as fuel to the internal combustion engine.
- the improved method of the present invention provides for reacting the methanol in a reactor comprising a monolithic substrate containing a plurality of substantially parallel channels and a plurality of passageways positioned through said monolithic substrate substantially parallel to said channels, said passageways containing a reforming catalyst, said channels being for the passage of heat exchange fluid through said monolithic substrate to supply heat to said monolithic substrate.
- the heat exchange fluid is preferably fluid heated in the internal combustion engine, for example engine exhaust gases or engine coolant.
- the heat exchange from the channels to the passageways of the monolithic substrate provides for waste heat recovery where internal combustion engine exhaust gases are used as the heat exchange fluid.
- This system is particularly well suited to the endothermic dissociation of methanol to H 2 and CO with a copper/zinc catalyst.
- This invention relates to monolithic substrate reactors for use in conducting catalytic exothermic reactions.
- This invention further relates to monolithic substrate reactors for conducting catalytic endothermic reactions.
- This invention further relates to a monolithic substrate reactor for conducting catalytic reactions wherein heat transfer means are positioned through the monolithic substrate for the transfer of heat from the substrate or for the transfer of heat to the substrate.
- the honeycomb of channels may be fabricated from glass, ceramics or metals or combinations thereof.
- the ceramic material may be selected from the group consisting of mullite (Al 6 Si 2 O 10 ), cordierite (Mg 2 Al 4 Si 5 O 18 ), alumina, silica, silicon carbide, silicon nitride, alkaline earth oxides, transition metal oxides, mixtures thereof, and glass.
- the metal may be selected from the group consisting of nickle, stainless steel, iron, aluminum, copper, titanium, alloys and mixtures thereof.
- the glass material may be selected from a group consisting of fused silica, flint glass, soda lime glass, alumino silicate glass, borosilicate glass, and mixtures thereof.
- a reactor comprising
- said monolithic substrate containing a plurality of substantially parallel channels completely through said monolithic substrate, and a plurality of passageways completely through said monolithic substrate generally parallel to said channels, said passageways being larger in cross-section and fewer in number than said channels, said passageways having catalytic material supported thereby,
- said distribution means comprising a plurality of passageway extensions parallel to said passageways and each said extension extending coaxially from a passageway and opening into a header chamber having a header chamber outlet, said header chamber outlet being in fluid flow communication with each of said passageways, said channels opening into a product chamber, said product chamber having a product outlet in fluid flow communication with each said passageway, said channels having channel walls and said passageways having passageway walls, said channel walls being integral with said passageway walls, each said passageway extension being connected to one of said passageways, each said passageway wall being mutually supporting with at least one said channel wall, and each said channel wall being mutually supporting with at least one other channel wall.
- FIG. 1 shows an embodiment of the present invention
- FIG. 2 is a cross-sectional view of the embodiment of the apparatus of the present invention shown in FIG. 1 taken along line 2--2;
- FIG. 3 is a schematic diagram of a process wherein the improved reactor of the present invention is useful.
- FIG. 4 is a schematic diagram of another process wherein the improved reactor of the present invention is useful.
- FIG. 5 is a perspective view of a preferred gas distributor for use in accordance with the invention.
- FIG. 6 is a partial top view of a preferred gas distributor.
- the reactor 10 comprises a casing 14 containing a monolithic substrate 12 which contains a plurality of small channels 18 as commonly used in such monolithic substrates.
- the channels 18 are positioned generally parallel through the substrate 12 with openings at each end of the substrate 12.
- the passageways 20 may contain catalytic pellets 1.
- the walls of passageways 20 may be coated with catalyst.
- the plurality of channels 18 are positioned through the substrate 12 for the passage of a heat exchange fluid therethrough. As shown in FIG. 1, the heat exchange fluid flows through channels 18 and is recovered via outlet 30.
- the channels 18 may have catalyst material therein, for example as a coating on the channel wall. This catalyst material may be selected to reduce pollutants in the heat exchange fluid.
- the heat exchange fluid is exhaust gas from the engine.
- the heat exchange fluid is introduced through a similar arrangement via a heat exchange fluid inlet 32.
- the reaction products are removed via a product outlet 24.
- the outlet 30 is positioned on one end of casing 14 to receive the heat exchange fluid flowing through the channels 18 into casing 14.
- the reactants are passed into passageways 20 via a reactant inlet 34.
- a variety of means for charging the reactants to the passageways 20 are known to the art and such means are suitable so long as substantially even flow is accomplished across the cross sectional area of substrate 12.
- a variety of gas distributor header means 7 can be used to recover the flow through passageways 20 for discharge through header chamber outlet 24.
- a reactant stream is charged to one end of substrate 12 via inlet 34 and passed therethrough under suitable reaction conditions to produce a product stream which is removed from the other end of substrate 12 via outlet 24.
- a heat exchange fluid is injected via heat exchange fluid inlet 32, passed through substrate 12 and recovered via outlet 30 to accomplish heat transfer in substrate 12. As shown in FIG. 1, the heat exchange fluid flows cocurrently with the reactants. In most instances it is anticipated that counter-current flow will be used although either type of flow was in the scope of the present invention.
- FIG. 2 is a cross-sectional view of the improved reactor of the present invention as shown in FIG. 1.
- FIG. 2 shows the small channels 18 positioned through substrate 12 and the passageways 20, positioned through substrate 12.
- channels 18 can be of any suitable configuration such as square, rectangular, round, triangular, etc. The configuration is normally chosen for convenience in fabrication or the like. The configuration of channels 18 is considered to be variable by those skilled in the art. Passageways 20 can also be of any suitable configurations.
- passageways 20 may be positioned through substrate 12 by drilling, by forming during the monolith substrate production process or the like. Further, conduits 20 may be formed with an extension from the ends of substrate 12 to permit the recovery of flow from passageways 20 or sleeves or the like may be sealingly positioned in the inlets and outlets of passageways 20. Further, tubular materials such as copper or the like could be used to extend through the entire length of substrate 12 to form passageways 20. The pellets 1 are then supported by the tubular element not shown. The particular method of fabrication may vary and any method of fabrication which results in the positioning of passageways 20 through substrate 12 for the flow of a reactant stream is considered suitable.
- the gas distributor header means 7 may be of a disc shape with tubular passageway extensions 8 extending therefrom.
- a screen 2 is provided for each passageway extension opening 9. These are as shown in FIGS. 5 and 6.
- the gas distributor header means 7 has passageway extensions 8 each having an outer cylindrical wall 4.
- the reactor 10 is symmetrical in that the same gas distribution header means is used on the inlet and outlet ends.
- Gas entering through heat exchange fluid inlet 32 passes into the heat exchange distribution fluid inlet chamber 3.
- the heat exchange fluid distribution inlet chamber 3 is defined by the cylindrical walls or of the passageway extensions 8 and the gas distributor plate reactor side wall 5.
- the gas distributor header has reactant inlet side wall 6.
- the reactant inlet side wall 6 forms a reactant inlet distribution chamber 22' with the inside wall of the casing 14.
- Reactant material entering through reactant inlet 34 passes into the passageway extensions 8 and continues on therethrough into the passageways 20. At the outlet end of the passageways 20 the gas again enters the passageway extensions 8. From the passageway extensions 8 the gas which has reacted over the catalytic material within the passageways then enters the header chamber 22 before passing out of the product outlet 24.
- the heat exchange fluid entering through the exchange fluid inlet 32 enters the chamber 3 and from there passes into and through the channels 18 into the chambers 3' wherein the heat exchange gaseous fluid collects and passes into the outlet 30.
- FIG. 3 is a schematic diagram of a process wherein the improved reactor of the present invention is considered useful.
- a methanol storage 30 is shown with a line 42 being positioned for the withdrawal of methanol therefrom.
- the methanol is typically liquid and is passed to a heat exchanger 44 where the methanol is vaporized and discharged as a vapor through a line 46 to a reactor 48, such as the improved reactor of the present invention, where the methanol is dissociated over a suitable reforming catalyst such as a copper/zinc base catalyst to produce hydrogen and carbon monoxide which are recovered through a line 50 and passed to a suitable combustion engine 52 where the carbon monoxide and hydrogen are combusted.
- a suitable reforming catalyst such as a copper/zinc base catalyst
- a free-oxygen containing stream is injected into engine 52 via a line 54 with the exhaust stream from engine 52 being recovered via a line 56 and passed back through reactor 48 as a heat exchange fluid where it provides the heat required by the endothermic dissociation reaction of methanol into carbon monoxide and hydrogen.
- the exhaust stream is then recovered via a line 58 and passed to further heat exchange with the liquid methanol in heat exchanger 44 after which it is discharged via a line 60.
- the reactor of the present invention is considered to be particularly suitable for such applications since it results in a relatively low pressure drop and since it is readily adapted to the use of heat exchange fluids.
- FIG. 4 is a schematic diagram of a further process in which the improved reactor of the present invention is useful.
- a heat source 70 which may be a carbonaceous fuel-fired plant, a nuclear reactor facility or the like, produces a heated stream which is discharged through a line 72 and passed to heat exchange with a reactant stream in a reactor 74 which is optionally of the type discussed above.
- the heat exchange fluid is recovered through a line 76 and passed back to plant 70 for reheating and the like.
- a suitable reactant stream charged to reactor 74 comprises methane and water. At least a portion of the water is added through a line 104.
- the methane is at least partially reformed into carbon monoxide and hydrogen over a suitable reforming catalyst such as those disclosed in U.S. Pat. No. 4,017,274.
- the resulting stream comprising carbon monoxide, hydrogen and optionally some methane, is passed via a line 80 through a heat exchanger 82 and to a remote location where it is reacted in a second reactor 86, which is optionally of the type discussed, to produce methane.
- the reaction conditions in reactor 86 are those known to the art for the production of methane and the catalyst used is a methanation catalyst.
- Such catalysts are considered to be well known to those skilled in the art as shown for instance in U.S. Pat. No. 3,890,113.
- the resulting product stream comprising methane is passed via a line 106 through a heat exchanger 88 and back to reactor 74.
- a line 106 In most instances it will be desirable to remove quantities of condensed water from line 106 downstream of heat exchanger 88 via a line 102.
- the water removed via line 102 will be substantially equivalent to that added via line 104 but since transportation over lone distances is contemplated, it is undesirable that the water remain in the pipeline system.
- heat from the power plant 70 is transferable over long distances via the closed system including reactors 74 and 86 which absorb heat via the chemical reactions occurring in reactor 74 with the heat being released in reactor 86 via the reactions occurring therein.
- a heat exchanger fluid is used to remove heat from reactor 86 with the heat exchange fluid being injected via a line 98 and recovered via a line 96 with heat being removed from the circulating heat exchange fluid via a heat exchanger 100.
- the heat exchange fluid flows counter-currently to the reactant stream.
- heat exchanger 88 is positioned to remove additional heat from the product gaseous stream with the heat being recovered by a heat exchange fluid injected via a line 90 and recovered via a line 92 with the heat being recovered from the circulating heat exchange fluid via a heat exchanger 94.
- heat is readily transferred from heat source 70 to a remote location where the heat is released at a desired location which may be an office building, a home or the like, wherein reactor 86 is positioned. It may not be necessary to include a heat exchanger such as heat exchanger 88 in the event that heat is effectively removed to the desired levels from reactor 86. Desirably flow to reactor 86 is controlled by a valve 84 to provide heat as required. Further, it is necessary that the flow rate to reactor 86 be controlled within reasonable limits to avoid damaging the catalyst etc. It will be noted that the process disclosed does not utilize streams in the catalytic reaction systems which contain contaminants.
- the system operates as a closed loop with the reactants being reacted repeatedly so that the addition of materials which would poison, contaminate or otherwise inactivate the catalyst surfaces is eliminated.
- heat is readily transferred from a central power source to a remote location.
- monolithic substrates as discussed herein is considered to be known to those skilled in the art as discussed, for instance, in the reference cited previously.
- the use of heat exchange means positioned in the monolithic substrate has not been known to the art heretofore to Applicant's knowledge. By the use of such heat exchange means, the efficiency of the catalyzed metal or ceramic monolith is greatly improved since the heat is removed from the substrate itself rather than through the casing or the like.
- the use of such monolithic substrates results in the ability to use high flow rates through the catalyst with relatively low pressure drops. Pressure drops much lower than those typically encountered with the use of fixed beds or fluidized beds are achieved.
- the fabrication of such monolithic substrates is well known to those in the art. As discussed in the article, monoliths having 400 to 600 cells per square inch are well known, although, as indicated previously, the particular monolith used is not considered to constitute a part of the present invention.
Abstract
Description
Claims (7)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
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US06/341,946 US4378336A (en) | 1979-12-18 | 1982-01-22 | Monolith reactor |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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US06/104,987 US4363787A (en) | 1979-12-18 | 1979-12-18 | Monolith heat exchange reactor |
US06/341,946 US4378336A (en) | 1979-12-18 | 1982-01-22 | Monolith reactor |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
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US06/104,987 Continuation-In-Part US4363787A (en) | 1979-12-18 | 1979-12-18 | Monolith heat exchange reactor |
Publications (1)
Publication Number | Publication Date |
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US4378336A true US4378336A (en) | 1983-03-29 |
Family
ID=26802144
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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US06/341,946 Expired - Fee Related US4378336A (en) | 1979-12-18 | 1982-01-22 | Monolith reactor |
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US (1) | US4378336A (en) |
Cited By (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4861347A (en) * | 1986-12-29 | 1989-08-29 | International Fuel Cells Corporation | Compact chemical reaction vessel |
US4929798A (en) * | 1984-03-05 | 1990-05-29 | Canadian Patents And Development Limited | Pseudoadiabatic reactor for exothermal catalytic conversions |
US5037619A (en) * | 1985-12-30 | 1991-08-06 | Institut Francais Du Petrole | Oxidization of an oxidizable charge in the gaseous phase and a reactor for implementing this method |
EP0661768A1 (en) * | 1993-12-28 | 1995-07-05 | Chiyoda Corporation | Method of heat transfer in reformer |
EP1155738A2 (en) * | 2000-05-18 | 2001-11-21 | Air Products And Chemicals, Inc. | Retrofit reactor including gas/liquid ejector and monolith catalyst |
US20040137288A1 (en) * | 2002-10-18 | 2004-07-15 | Monsanto Technology Llc | Use of metal supported copper catalysts for reforming alcohols |
US6790417B2 (en) | 2000-12-21 | 2004-09-14 | Corning Incorporated | Monolith loop reactors |
US20050135978A1 (en) * | 2003-10-14 | 2005-06-23 | Mourad Hamedi | Method and apparatus for optimizing throughput in a trickle bed reactor |
US20050159305A1 (en) * | 2000-04-11 | 2005-07-21 | Monsanto Company | Catalyst for dehydrogenating primary alcohols |
US20050223891A1 (en) * | 2002-01-08 | 2005-10-13 | Yongxian Zeng | Oxy-fuel combustion process |
WO2006100176A1 (en) * | 2005-03-23 | 2006-09-28 | Alstom Technology Ltd | Method and device for combusting hydrogen in a premix burner |
US20080010993A1 (en) * | 2006-06-13 | 2008-01-17 | Monsanto Technology Llc | Reformed alcohol power systems |
KR20080060871A (en) * | 2006-12-27 | 2008-07-02 | 유니슨 주식회사 | Multi layer catalyst reactor equipped with metal monolith heat exchanger for hydrocarbon steam reforming and producing method of hydrogen gas using the multi layer catalyst reactor |
US20090142239A1 (en) * | 2005-07-21 | 2009-06-04 | Kohei Yoshida | Exhaust purification apparatus of internal combustion engine |
EP2092977A2 (en) * | 2008-02-14 | 2009-08-26 | Ngk Insulators, Ltd. | Plasma reactor with a honeycomb electrode |
WO2009141517A1 (en) * | 2008-05-23 | 2009-11-26 | Ifp | Novel bayonet-tube heat exchanger reactor, the tubes of which are surrounded by shafts in cement |
WO2010128006A1 (en) * | 2009-05-04 | 2010-11-11 | Shell Internationale Research Maatschappij B.V. | Cooling module and reactor comprising the same |
ITMI20090826A1 (en) * | 2009-05-13 | 2010-11-14 | Eni Spa | REACTOR FOR EXOTHERMIC OR ENDOTHERMAL CATALYTIC REACTIONS |
US20130034785A1 (en) * | 2009-12-14 | 2013-02-07 | Intelligent Energy, Inc. | Hydrogen generation utilizing integrated co2 removal with steam reforming |
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-
1982
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US4101287A (en) * | 1977-01-21 | 1978-07-18 | Exxon Research & Engineering Co. | Combined heat exchanger reactor |
US4221763A (en) * | 1978-08-29 | 1980-09-09 | Cities Service Company | Multi tube high pressure, high temperature reactor |
Non-Patent Citations (1)
Title |
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Cited By (46)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4929798A (en) * | 1984-03-05 | 1990-05-29 | Canadian Patents And Development Limited | Pseudoadiabatic reactor for exothermal catalytic conversions |
US5037619A (en) * | 1985-12-30 | 1991-08-06 | Institut Francais Du Petrole | Oxidization of an oxidizable charge in the gaseous phase and a reactor for implementing this method |
US4861347A (en) * | 1986-12-29 | 1989-08-29 | International Fuel Cells Corporation | Compact chemical reaction vessel |
EP0661768A1 (en) * | 1993-12-28 | 1995-07-05 | Chiyoda Corporation | Method of heat transfer in reformer |
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